201012918 六、發明說明： 本發明有關一諸如通常發生於煤氣化反應中之合成氣 體的生產期間將灰塵除氣之設備，在此所使用之合成氣體 思才s具有寬廣變化之純度而被用於不同化學合成物的氣體 混合物，且除了一氧化碳及氫以外，通常亦以變化之組合 包含二氧化碳、氮、硫化氫、及其他成份。該等灰塵被除 氣’以致該灰塵中所包含之毒性氣體完全地不再造成環境 之公害。該如此獲得之尾氣可藉由該設備所收集及由該系 統排出。藉著該設備按照本發明，其係可能利用該等灰塵 中所包含之剩餘熱及冷卻所獲得之灰塵。於除氣期間，該 等灰塵之壓力被該設備由通常於煤氣化反應期間普及之高 壓位準減少至普通之大氣壓力。本發明亦因此有關一製 程’由此來自合成氣體之灰塵能被滌氣及完全地或幾乎完 全地除氣。 諸如寬廣變化性之煤、泥炭、液化殘渣、其他殘渣、 廢料、生物物質、及飛灰、或這些材料之混合物的固體燃 料之熱氣化’係在升高之壓力及高溫下施行，並具有以一 高能量含量及/或以一適合用於隨後的化學合成物之成份 產生一原始合成氣體之目標。該原始之合成氣體係裝滿飛 灰，該飛灰源自該燃料供給之飛灰含量。該飛灰係呈微粒 之形式，其需要在隨後的使用之前被分離出去。以乾燥分 離，譬如於一旋風分離器或一過濾器中，該很細之粒狀固 體通常在由該壓力室排出之前積累。本來，於微粒之堆積 的空隙份額中有氣體，於此案例+，被排出之原始合成氣 201012918 體具有該固體。在最後儲存或移除之前，該固體必須減少 壓力，且仍然於該空隙份額中之原始合成氣體被移除。201012918 VI. Description of the Invention: The present invention relates to a device for degassing dust during the production of a synthesis gas which usually occurs in a coal gasification reaction, and the synthetic gas used herein has a broadly varying purity and is used. Gas mixtures of different chemical compositions, in addition to carbon monoxide and hydrogen, typically also contain carbon dioxide, nitrogen, hydrogen sulfide, and other components in varying combinations. The dust is degassed so that the toxic gases contained in the dust are completely no longer harmful to the environment. The offgas thus obtained can be collected by the apparatus and discharged by the system. According to the present invention, it is possible to utilize the residual heat contained in the dust and the dust obtained by the cooling. During degassing, the pressure of such dust is reduced by the apparatus from a high pressure level that is generally prevalent during the coal gasification reaction to normal atmospheric pressure. The invention is thus also related to a process whereby dust from the synthesis gas can be scrubbed and completely or almost completely degassed. Thermal gasification of solid fuels such as broadly variable coal, peat, liquefied residue, other residues, waste, biomass, and fly ash, or mixtures of these materials, is carried out under elevated pressure and elevated temperatures, and A high energy content and/or a target for producing a raw synthesis gas in a composition suitable for use in subsequent chemical compositions. The original syngas system is filled with fly ash which is derived from the fly ash content of the fuel supply. The fly ash is in the form of microparticles which need to be separated prior to subsequent use. In the case of dry separation, such as in a cyclone or a filter, the very fine granular solids are usually accumulated before being discharged from the pressure chamber. Originally, there is a gas in the void fraction of the accumulation of particles, and in this case +, the original syngas that is discharged is 201012918. Prior to final storage or removal, the solid must reduce the pressure and still remove the original synthesis gas in the void fraction.
相對於來自一煤氣化製程之合成氣體的滌氣所建立之 相關尖端技術係敘述於美國專利第4,838,898A號中。美國 專利第2007/00841 17A1號說明用於合成氣體之另一生產製 程，其將由一煤氣化反應器所獲得之合成氣體連續地引導 經過一系統，以與一較冷之外來氣體混合，且說明一熱交 換器及一灰塵分離器。該灰塵分離器可被配備有一用於淨 化乳體之進給裝置。在此於該壓力下降系統之下游可有數 個隨後之灰塵分離器，以達成一較大之產量。這在重疊之 間隔以一淨化氣體允許批量飛灰之透過作用，以便於該等 進料斗之倒空及充填期間移除該不想要之氣體。 該剝離製程將被當作一時間決定步驟。被設立之製程 提供用於該飛灰堆疊之透過作用，以排除任何殘餘的原始 合成氣體成份。為什麼所設立之製程花費長時間的主要理 由之一係於透過作用期間在與於重力相反之方向中，通常 形成通道，當該氣體速度増加時，由於該飛灰之彳艮細的微 粒尺寸，該氣體貫穿經過該等通道。由於此不均勻的透過 作用，其交換該整個空隙份額中之氣體所花費的時間之 量增加。在與於重力相反之方向巾，於透過作用期； 由於該細微顆粒的堆積壓實及該作為後果產 . . J网流動P且 力之風險，其在由該進料斗倒空或移除期間造成門 因此，該目的係提供_設備，其將來自 之合成氣體的飛灰逐步地返回至大氣壓力，且移除誃飛灰 7 201012918 中所包含之合成氣體。使用該設備所進行的製程之目的係 亦交換及返回該氣體，該氣體於該倒空及充填製程期間累 積在該壓力下降容器及除塵器中。 本發明達成在一設備之形式中將來自一由氣化製程所 產生之合成氣體的灰塵除氣之目的，該設備包括： •一主要灰塵分離器， •一多用途容器， •用於除氣及冷卻之流體， •一用於灰塵之儲存設備， •所生產之合成氣體經由一連接管子被引導至一主要 灰塵分離器，已除塵之原始合成氣體氣流及塵狀的固體玎 被由該主要灰塵分離器移除，該塵狀的固體亦仍然於該等 灰塵微粒間之空隙中包含原始之合成氣體， •該塵狀的固體被引導進入配備有用於減少該壓力位 準之裝置的多用途容器，以致獲得一尾氣，且留下一於該 空隙份額中包含較低氣體數量之固體， •有一用於將固體運送進入氣體交換設備之裝置，該 氣體交換設備包括： •一氣體交換槽， •一灰塵分離器， •一用於交換氣體之進給裝置， •其係可能將該氣體交換槽減少至大氣壓力， •該氣體交換設備具有用於一固體之出口，該固體已 至少局部地由原始之合成氣體釋出， 201012918 該氣體交換設備具有一往上導向之輸送帶，一往上 導引之氣體及固體粒子流能被建立在該輸送帶中， 輸送帶具有打開之橫截面、一底部有效截面及 一頂部有效截面， 該輸送帶之底部有效戴面被包圍在接近該底部之氣 體交換槽内， — 一引導進入該底部有效截面之交換氣體進給裝置被 疋位在該輸送帶之底部端部的下方， ❹ 灰塵分離器係以此一使得其能以來自豸氣體交換 槽的氣體及固體粒子流所供給之方式連接，及 該灰塵分離器具有一用於尾氣氣流之排出裝置及一 進入該氣體交換槽之往下引導連接裝置，該氣體交換槽用 於一由原始合成氣體所釋出之固體。 該設備的一實施例設想於該加工流程中之任何點在該 。又備中有熱交換器’該熱交換器被設計成為一冷卻器， 且被定位，以致其冷卻表面係與該塵狀的固體接觸。較佳 地是，至少一個此冷卻器係坐落在該氣體交換設備中。在 該設備内，&-冷卻器彳為於該灰塵分離器及該氣體交換 槽間之連接裝置中坐落在該加工流程中、或直接地在該氣 體交換槽；各種組合係亦可能的。 該設備之其他實施例設想該灰塵儲存設備具有一壓力 均衡作用m係、連接至該氣體交換設備t灰塵分離 器；該氣體交換槽及該灰塵分離器亦可形成單一結構單元。 本發明進一步藉著一製程達成將來自一合成氣體的灰 201012918 塵除观之目的，該合成氣體被—氣化製程所生產，且通常 包含一氧化碳及氫氣'以及灰燼與灰塵微粒，其中 .所生產之合成氣體係經由一連接管子引導進入一主 要灰塵刀離器’大多數該灰塵係在該主要灰塵分離器中分 離出去， •一旦該灰塵已被分離出去，該等固體粒子流在該相 同之壓力位準被引導進入一多用途容器，該固體粒子流係 在該多用途容器中減少壓力’以致獲得一尾氣氣流，且留 下一於該空隙份額中包含較低氣體數量之固體， •該固體粒子流係藉著運送氣體由該多用途容器氣動 地引導進入一氣體交換設備，及 ’一固體循環粒子流係藉著一交換氣體在該氣體交換 設備内生產，及 •所釋出之尾氣藉此係經由一灰塵分離器排出。 用於該冷卻，於該灰塵分離器及該氣體交換槽間之連 接裝置中’該製程之其他實施例設想該灰塵在該加工流程 中被冷卻。其亦可設想該灰塵係在該氣體交換槽中被冷卻。 該製程之另一實施例設想該多用途容器及氣體交換槽 間之運送管線中的運送密度係少於該塵狀固體之堆積密度 的百分之75。 該製程之另—實施例設想與該下一批量之有空隙氣體 的一部份同時，藉由加入交換氣體在該多用途容器中移除 该氣體交換槽中之批量處理。 另—選擇係，該製程之其他實施例設想被強迫進入該 201012918 多用途容器、該氣體交換槽的其中之一或兩者的交換氣 體’係連續地或批次地、循環往復地或跳動地於該氣體交 換製程期間被加入。 另一選擇係’該製程之其他實施例設想被加入之交換 氣體係隨同在該空隙空間中之至少部份該原始合成氣體， 由該多用途容器或該氣體交換槽的其中之一批次地或連續 地排出。在所有案例中，該加入與排出操作可被分開地及 連續地或批次地進行，由於如此達成之製程彈性，其係本 〇 發明的一優點。 該製程之其他實施例有關離開該設備之氣體。在此， 其可被設想一旦該交換氣體已由該循環固體分離及已離開 該氣體交換設備’加至該氣體交換槽之交換氣體係隨著該 空隙空間中之至少部份該原始合成氣體餵入至一處置單 元。其亦可設想由該多用途容器所排出之氣體係餵入至一 處置單元。其可進一步設想一旦該交換氣體已由該循環固 體分離及已離開該氣體交換設備，所加入之交換氣體係隨 ® 著該空隙空間中之至少部份該原始合成氣體餵入至一燃燒 反應器，且由該多用途容器所排出之氣體係餵入至一燃燒 反應器。其可進一步設想在由該循環固體分離之後及在離 開該氣體交換設備之後，隨同該空隙空間中之至少部份該 原始合成氣體所加入的交換氣體、或由該多用途容器所排 出之氣體、或兩氣體首先被餵入至一用於緩衝及均衡作用 之儲氣器。 所敘述之設備及所敘述之製程提供來自一煤氣化製程 11 201012918 的飛灰之快速及完全除氣的優點。所敘述之製程可顯著地 減少用於飛灰的除氣所需要之時間。 按照本發明之設備係基於三圖示所說明，這些圖示僅 只是按照本發明之設備的設計之範例。 圖1顯示被設計用於合成氣體的出口噴嘴下游之灰塵 的除氣作用之設備的整個零件。 圖2顯示具有該氣體交換槽1〇及該附屬之灰塵分離器 13的氣體交換設備21。 圖3顯示具有一整合式灰塵分離器13之氣體交換槽 ❿ 10 ° 包含飛灰1之經加壓的原始合成氣體被引導進入該飛 灰分離器3,該飛灰分離器可被設計成為一過濾器或一旋風 分離器。如此獲得一已除塵之合成氣趙2及飛灰4，該飛灰 被引導進入該多用途容器5。於如此做中，其係不可避免使 微粒堆積的空隙份額中之小數量原始合成氣體亦進入該多 用途容器5。於該多用途容器5中’仍然被加壓之飛灰的壓 力係減少。然後該批量之固體7藉由加入運送氣體8經由 © 一氣動運送管線9被運送進入該氣體交換設備21之氣體交 換槽10。為了補償由該多用途容器5所運送的固體之體積 及為了維持該多用途容器5中之高壓，交換氣體6被餵入 該多用途容器5’該多用途容器5在該飛灰之排出期間具有 一吹風容器之作用。 當該抵量已被運送至該氣體父換槽10時，交換氣體11 被加入，使得一往上導引之氣體及固體粒子流12接踵而 12 201012918 來。此氣體及m體粒子流進入一分_，該@體係在該分 離器中由該氣體分離，故該固體14往下返回朝向其出發之 地點，在此該往上導引之氣體及固體粒子流12係藉由加入 氣體11所產生。這樣一來達成該固體之循環，該固體之循 環能經由該氣體交換槽10之幾何形狀的設計、且特別經由 該氣體餵入器11被控制。已由該固體被釋出之氣體以連續 或批次模式的其中之一離開該氣體交換槽丨〇。 實際上，簡單之標準透過作用需要一相當可觀之時間 數置，因由於該很細微之塵狀微粒，僅只非理想之透過作 用旎被達成，該理由係譬如溝道作用及阻塞。於已藉由該 固體之運動所放鬆的堆積及所加入的洗滌氣體之間，按照 本發明結合一洗滌氣體流及該固體之循環達成最佳之氣體 父換。該固體之強烈的向上粒子流確保該空隙份額中之氣 體的最佳可能暴露至該交換氣體及混合該二者。該空隙份 額中之原始合成氣體成份的想要或可採納的剩餘濃度可關 於所加入之氣體11的數量經由該固體之循環次數輕易地達 w 成。 以下由該原始之合成氣體分離’於大部份之案例中， 該固體之溫度係太高，以致不能被儲存或移除甚至在其已 被傳送至該氣體交換槽之後。因此，提供熱傳送裝置該 熱傳送裝置與該循環之固體接觸，並消散熱量，以達成該 固體之目標溫度。在本範例中，這是該熱交換器丨5。 已被除氣至該最大可能程度之飛灰係由氣體交換設備 21獲得，且經由一排出系統16餵入至一圓筒倉17。該圓 13 201012918 筒倉17係配備有一均衡作用管線2〇,該均衡作用管線使充 填期間所位移之氣體返回至該灰塵分離器13。此外，一由 該灰塵分離器13所獲得之尾氣18係以與由該多用途容器5 所獲得之已除塵的尾氣19相同之方式處理。 圖2顯示一外部固體循環回路。在此，來自該氣體交 換槽10的往上導引之氣體及固體粒子流12係藉由加入交 換氣體11被導引至一灰塵分離器13。在此，該固體係由該 氣體分離’該氣體包括所加人之交換氣體U及來自微粒之 堆積的空隙份額之氣體的混合物。該氣體混合物18被健入 至-處置單元。該已分離之固體於重力之方向中往下流動 朝向該氣體交換槽1G。呈平板型之熱交換器15係在該往下 粒子流中設計成為-熱傳送表面，以便消散該固體之熱量。 圖3顯示該相同之原理，但具有内部之循環亦即該 固體粒子流在該氣體交換槽1〇内循環。於此案例中，根據 树明之設備的氣體交換槽1()係配備有—整合式灰塵分離 器13。再者’熱傳送表面被提供用於冷卻該固體。用於熱 傳送’呈冷卻罩套之形式的二有夾層的壁面被提供當作熱 交換器15 〇於此案例中，坊楚無乂由、试士 千列甲"亥等熱傳送表面應於操作期間被 浸入該循環固體中。 其他範例提及操作之模式。於—較佳製程模式中與 首先在該氣趙交換槽1G中處理的—批量同時地使用該多用 途容器5，以減少將被承接夕 艰接之下一批量的壓力，隨後空隙份 額氣體逃離，且然後，於該剎铪卩主M # 於孩剩餘時間期間，再次藉著該氣 體飯入管線6升商該麼力，为接办v东 及後來又馬上減少該壓力。加 201012918 塵作用造成該空隙份額中之眉 ^ ^ , ^之原始合成氣體含量的稀釋；壓 Γ之減少㈣接著存在之部份該氣體混合物。視可用之 時間而定，此程序能被重複數 .Μ ^ , 欠以致部份該原始之合成 :體係由該㈣份額排除，甚至在該等固體批量被運送至 體交換槽10供處理之前。這減少該氣體 ，：體的循環之次數，如此縮短該循環時間。因此，每單 位時間之較大數量的飛•方的站山斗β #其 00 b由該原始之合成氣體釋出及 7 P，儘3有該單一管線配置。 用途在此中被稱為—多用途容器5,因為其具有各種 用途之作用。首弁，JL直女 _ . 製程底進料之仙，用於在 位準承接批量之固體及用於減少此麼力位準。其 :::一：先洗蘇階段之作用，以藉由循環的加壓作用及 之：少自該堆積預先移除部份該原始之合成氣體， 體二槽中具有一吹風容器之作用，用於氣動運送至該氣 體父換槽中之主要洗滌階段。 ❺ 之惰換氣體6及11及該運送氣體8亦可包括諸如氮 但空氣、二氧化碳等亦可被使用。如果該氣 子流18係傲入至一後燃燒單元，譬如使用空氣 耗。"換氣體U可為有利的，且亦促成減少惰性氣體消 之一倦此未顯不之用於該等尾氣18及19的下游處置單元 -優點係幾乎連續地操作該主要 :::隔所中斷，該下-批量係在該等時間間二= 則送帶所運送。該結果係以數量之觀點，發生一幾乎 15 201012918 恆定之尾氣18氣流’由該製程之觀點，其處理係、比於 操作期間發生數量峰值之案例更容易。 該預先洗滌階段之另一有利製程變型在於該批量不是 以交換氣體循環往復地加壓與接著在壓力中減少，但在$ 定之壓力以一連續之粒子流加壓。如此，在此將無下降之 氣流峰值，且用於尾氣氣流18及19之處置單元將被以來 自該預先洗滌階段及該主要洗滌階段之連續粒子流加壓。 【主要元件符號說明】 1 原始合成氣體 2 已除塵之原始合成氣體 3 飛灰分離器 4 飛灰排出 5 多用途容器 6 交換氣體 7 用於將飛灰局部地除氣之排出線管 8 運送氣體 9 氣動運送管線 1 〇氣體交換槽 11交換氣體 12往上導引之氣體及固鱧粒子流 13灰塵分離器 14固體 1 5熱交換器 1 6排出系統 16 201012918 17圓筒倉 18尾氣 19尾氣 20均衡作用管線 2 1氣體交換設備Related advanced techniques established with respect to scrubbing of a synthesis gas from a coal gasification process are described in U.S. Patent No. 4,838,898 A. US Patent No. 2007/00841 17A1 describes another production process for synthesis gas that continuously directs synthesis gas obtained from a coal gasification reactor through a system for mixing with a cooler external gas, and illustrates A heat exchanger and a dust separator. The dust separator can be equipped with a feeding device for purifying the milk. There may be several subsequent dust separators downstream of the pressure drop system to achieve a larger throughput. This allows a bulk fly ash to pass through at a time interval of overlap with a purge gas to facilitate removal of the unwanted gas during emptiness and filling of the feed hopper. This stripping process will be treated as a time decision step. The established process provides for the permeation of the fly ash stack to exclude any residual raw syngas components. One of the main reasons why the established process takes a long time is that during the action, in the opposite direction to gravity, the channel is usually formed. When the gas velocity is increased, due to the fine particle size of the fly ash, The gas passes through the channels. Due to this uneven permeation, the amount of time it takes to exchange the gas in the entire void fraction increases. In the opposite direction of gravity, in the period of permeation; due to the compaction of the fine particles and the consequences of the production. J network flows P and the risk of force during the emptying or removal of the feed hopper This is the purpose of providing a device that progressively returns the fly ash from the synthesis gas to atmospheric pressure and removes the synthesis gas contained in the fly ash 7 201012918. The purpose of the process performed using the apparatus is to also exchange and return the gas which accumulates in the pressure drop vessel and the precipitator during the emptying and filling process. The invention achieves the purpose of degassing dust from a synthesis gas produced by a gasification process in the form of a device comprising: • a primary dust separator, • a multipurpose container, • for degassing And cooling fluid, • a storage device for dust, • the synthetic gas produced is directed to a main dust separator via a connecting pipe, the dust-removed raw syngas gas stream and dusty solid helium are The dust separator is removed, the dusty solid still contains the original synthesis gas in the gap between the dust particles, • the dusty solid is directed into a multipurpose device equipped with means for reducing the pressure level The vessel is such that an off-gas is obtained and a solid containing a lower amount of gas in the void fraction is left, • a means for transporting the solids into the gas exchange apparatus, the gas exchange apparatus comprising: • a gas exchange tank, • a dust separator, • a feed device for exchanging gases, • it may reduce the gas exchange tank to atmospheric pressure, • The gas exchange apparatus has an outlet for a solid that has been at least partially released from the original synthesis gas, 201012918. The gas exchange apparatus has an upwardly directed conveyor belt, a gas and solid particles directed upward Flow energy is established in the conveyor belt, the conveyor belt has an open cross section, a bottom effective section and a top effective section, and the bottom effective belt surface of the conveyor belt is enclosed in a gas exchange tank close to the bottom, The exchange gas feed device leading into the effective section of the bottom is clamped below the bottom end of the conveyor belt, and the dust separator is such that it can flow with gas and solid particles from the helium gas exchange tank. The supply is connected, and the dust separator has a discharge device for the exhaust gas flow and a downward guide connection device for entering the gas exchange groove for a solid released from the raw synthesis gas. An embodiment of the apparatus is contemplated at any point in the processing flow. There is also a heat exchanger. The heat exchanger is designed as a cooler and is positioned such that its cooling surface is in contact with the dusty solid. Preferably, at least one such cooler is located in the gas exchange apparatus. Within the apparatus, the &-cooler is located in the process flow or directly in the gas exchange tank between the dust separator and the gas exchange tank; various combinations are also possible. Other embodiments of the apparatus envisage that the dust storage device has a pressure equalization m system coupled to the gas exchange device t dust separator; the gas exchange tank and the dust separator may also form a single structural unit. The invention further achieves the purpose of removing the ash 201012918 from a synthesis gas by a process, the synthesis gas is produced by a gasification process, and usually contains carbon monoxide and hydrogen 'and ash and dust particles, wherein The syngas system is guided through a connecting pipe into a main dust cutter. Most of the dust is separated in the main dust separator. • Once the dust has been separated, the solid particles flow in the same The pressure level is directed into a multi-purpose container that reduces the pressure in the multi-purpose container such that a tail gas stream is obtained and a solid containing a lower amount of gas in the void fraction is left. The solid particle flow is pneumatically guided from the multi-purpose container into a gas exchange device by means of a carrier gas, and 'a solid circulating particle stream is produced in the gas exchange device by means of an exchange gas, and the exhaust gas released Thereby it is discharged via a dust separator. For this cooling, in the connection between the dust separator and the gas exchange tank, other embodiments of the process envisage that the dust is cooled in the process flow. It is also conceivable that the dust is cooled in the gas exchange tank. Another embodiment of the process envisages that the transport density in the transport line between the multi-purpose container and the gas exchange tank is less than 75 percent of the bulk density of the dusty solid. Another embodiment of the process envisages removing the batch processing in the gas exchange tank in the multi-purpose vessel by adding an exchange gas simultaneously with a portion of the next batch of voided gas. Alternatively, the selection system, other embodiments of the process envisage forced exchange into the 201012918 multi-purpose vessel, one or both of the gas exchange tanks, continuously or batchwise, cyclically or beatingly It was added during the gas exchange process. Another option is that the other embodiment of the process envisages that the added exchange gas system is accompanied by at least a portion of the raw synthesis gas in the void space, from the multi-purpose container or one of the gas exchange tanks. Or discharge continuously. In all cases, the joining and discharging operations can be carried out separately and continuously or in batches, which is an advantage of the invention due to the process flexibility thus achieved. Other embodiments of the process relate to gases leaving the apparatus. Here, it can be envisaged that once the exchange gas has been separated by the circulating solids and has left the gas exchange device, the exchange gas system added to the gas exchange tank is fed with at least a portion of the original synthesis gas in the void space. Enter into a disposal unit. It is also conceivable that the gas system discharged from the multi-purpose container is fed to a disposal unit. It may further be envisaged that once the exchange gas has been separated from the recycle solids and has exited the gas exchange apparatus, the added exchange gas system feeds the raw synthesis gas to a combustion reactor along with at least a portion of the void space And the gas system discharged from the multi-purpose container is fed to a combustion reactor. It may further envisage, after separation from the circulating solids and after exiting the gas exchange apparatus, the exchange gas with which at least a portion of the raw synthesis gas is added, or the gas discharged from the multipurpose container, Or the two gases are first fed to a gas reservoir for buffering and equalization. The described apparatus and the described process provide the advantages of rapid and complete degassing of fly ash from a coal gasification process 11 201012918. The described process can significantly reduce the time required for degassing of fly ash. The apparatus according to the invention is illustrated on the basis of three figures, which are merely examples of the design of the apparatus according to the invention. Figure 1 shows the entire part of the apparatus for the degassing of dust downstream of the outlet nozzle designed for synthesis gas. Fig. 2 shows a gas exchange device 21 having the gas exchange tank 1 and the associated dust separator 13. Figure 3 shows a gas exchange tank with an integrated dust separator 13 10 ° The pressurized raw synthesis gas containing fly ash 1 is directed into the fly ash separator 3, which can be designed as a Filter or a cyclone separator. Thus, a dust-removed syngas Zhao 2 and fly ash 4 are obtained, which is guided into the multi-purpose container 5. In doing so, it is inevitable that a small amount of the raw synthesis gas in the void fraction of the particulate accumulation also enters the multipurpose container 5. In the multi-purpose container 5, the pressure of the fly ash which is still pressurized is reduced. The batch of solids 7 is then transported into the gas exchange tank 10 of the gas exchange unit 21 via a pneumatic conveying line 9 by the addition of a carrier gas 8. In order to compensate for the volume of solids transported by the multi-purpose container 5 and to maintain the high pressure in the multi-purpose container 5, the exchange gas 6 is fed into the multi-purpose container 5'. The multi-purpose container 5 is discharged during the fly ash. It has the function of a hair dryer. When the offset has been transported to the gas parent shifting tank 10, the exchange gas 11 is added such that a gas and solids stream 12 directed upwards is followed by 12 201012918. The gas and the m-body particle stream enter a fraction, and the @ system is separated by the gas in the separator, so that the solid 14 is returned downward toward the starting point where the gas and solid particles are directed upward. Stream 12 is produced by the addition of gas 11. In this way, the circulation of the solid is achieved, the circulation of the solid can be controlled via the geometry of the gas exchange tank 10, and in particular via the gas feeder 11. The gas that has been released from the solid exits the gas exchange tank in one of a continuous or batch mode. In fact, the simple standard permeation requires a considerable amount of time, because the very fine dust particles are only achieved by non-ideal permeation, such as channeling and blocking. Between the accumulation which has been relaxed by the movement of the solid and the added scrubbing gas, an optimum gas mastering is achieved in accordance with the present invention in combination with a flow of scrubbing gas and circulation of the solid. The strong upward particle flow of the solid ensures that the gas in the void fraction is optimally exposed to the exchange gas and to mix the two. The desired or acceptable residual concentration of the raw syngas component in the void fraction can be readily achieved by the number of cycles of the solids 11 added. The following is the separation of the original synthesis gas. In most cases, the temperature of the solid is too high to be stored or removed even after it has been transferred to the gas exchange tank. Accordingly, a heat transfer device is provided which contacts the solid of the cycle and dissipates heat to achieve a target temperature of the solid. In this example, this is the heat exchanger 丨5. The fly ash that has been degassed to this maximum extent is obtained by the gas exchange unit 21 and fed to a cylindrical chamber 17 via a discharge system 16. The circle 13 201012918 The silo 17 is equipped with an equalization line 2〇 which returns the gas displaced during the filling to the dust separator 13. Further, an exhaust gas 18 obtained by the dust separator 13 is treated in the same manner as the dust-removed exhaust gas 19 obtained by the multi-purpose container 5. Figure 2 shows an external solids circulation loop. Here, the upwardly directed gas and solids stream 12 from the gas exchange tank 10 is directed to a dust separator 13 by the addition of the exchange gas 11. Here, the solid is separated by the gas. The gas includes a mixture of the exchange gas U of the added person and the gas from the void portion of the particles. The gas mixture 18 is brought into the treatment unit. The separated solid flows downward in the direction of gravity toward the gas exchange tank 1G. A flat plate type heat exchanger 15 is designed as a heat transfer surface in the downward flow of particles to dissipate the heat of the solid. Figure 3 shows the same principle, but with an internal circulation, i.e., the flow of solid particles circulates within the gas exchange tank 1〇. In this case, the gas exchange tank 1 () according to Shuming's equipment is equipped with an integrated dust separator 13. Again the 'heat transfer surface is provided for cooling the solid. A two-layered wall for heat transfer 'in the form of a cooling jacket is provided as a heat exchanger 15 〇 In this case, the heat transfer surface of the tester It is immersed in the circulating solid during operation. Other examples mention the mode of operation. In the preferred process mode, the multi-purpose container 5 is used simultaneously with the batch processed first in the gas exchange tank 1G to reduce the pressure that will be accepted under a batch, and then the void share gas escapes. And then, during the remaining time of the brakes, the M # is again used by the gas to enter the pipeline 6 to promote the force, in order to take over the v East and then immediately reduce the pressure. Adding 201012918 Dust effect causes dilution of the original synthesis gas content of the eyebrows ^ ^ , ^ in the void fraction; reduction of pressure enthalpy (4) followed by the portion of the gas mixture. Depending on the time available, the program can be repeated by a number of Μ ^ , owing to some of the original synthesis: the system is excluded from the (four) share, even before the solid batch is shipped to the body exchange tank 10 for processing. This reduces the number of cycles of the gas, body, and thus shortens the cycle time. Therefore, a larger number of flying squares of each side of the unit's station, β#, 00b, are released from the original synthesis gas and 7 P, which has the single pipeline configuration. The use is referred to herein as a multi-purpose container 5 because it has a variety of uses. First, JL Straight Female _ . The bottom of the process feed, used to take the bulk of the solids at the level and used to reduce this level of force. Its::: one: the role of the first washing stage, by the pressure of the circulation and: less pre-removed part of the original synthesis gas from the accumulation, the body has a blowing container in the two slots, It is used for pneumatic transport to the main washing stage in the gas shifting tank. The inert gas exchange gases 6 and 11 and the carrier gas 8 may also include, for example, nitrogen but air, carbon dioxide or the like may also be used. If the gas stream 18 is directed to a post-combustion unit, such as air consumption. " Changing the gas U can be advantageous, and also contributes to reducing the inert gas consumption, which is not apparent for the downstream disposal units of the exhaust gases 18 and 19 - the advantage is that the main operation is almost continuously:: Interrupted, the lower-batch is carried during the time two = then the belt is transported. This result is based on the quantity, and an almost exhausted 18 gas flow occurs almost 15 201012918. From the viewpoint of the process, the processing system is easier than the case where the number of peaks occurred during the operation. Another advantageous process variant of the pre-wash stage is that the batch is not reciprocally pressurized with an exchange gas cycle and then reduced in pressure, but is pressurized at a constant pressure with a continuous stream of particles. Thus, there will be no peaks in the descending gas flow, and the treatment unit for the tail gas streams 18 and 19 will be pressurized by the continuous stream of particles from the pre-wash stage and the main wash stage. [Main component symbol description] 1 Raw synthesis gas 2 Dedusted raw synthesis gas 3 Fly ash separator 4 Fly ash discharge 5 Multipurpose container 6 Exchange gas 7 Discharge line tube 8 for partially degassing fly ash 9 Pneumatic transport line 1 〇 Gas exchange tank 11 Exchanging gas 12 upwards directed gas and solid particle flow 13 Dust separator 14 Solid 1 5 Heat exchanger 1 6 Discharge system 16 201012918 17Cylinder 18 exhaust 19 exhaust 20 Equilibrium line 2 1 gas exchange equipment